Process and apparatuses for preparing nanoparticle compositions with amphiphilic copolymers and their use

ABSTRACT

This invention discloses a process for making nanopanticles of amphiphilic copolymers by flash precipitation. Nanoparticles may be of amphiphilic copolymer alone or may contain an additive target molecule, preferably an organic active. The inclusion of additive target molecules in amphiphilic copolymer nanoparticles can alter their water solubility characteristics, fluid dynamics, and/or stability. Changing an additive target molecule&#39;s solubility and stability in an nanoparticle can make a water insoluble compound suitable for pharmaceutical administration as well as specifically target the molecule to a specific area of a patient&#39;s body. The process affords the production of nanoparticles at high absolute active content, at high yield, high productivity, and high processing rates while using unusually low amounts of amphiphilic copolymers. Furthermore, the resulting particles exhibit sufficient stability for post processing as desired. The invention also discloses two apparatuses for the production of nanoparticles of amphiphilic copolymers by flash precipitation.

RELATED APPLICATIONS

The present application claims priority from pending provisionalapplication 60/280,433 filed Mar. 30, 2001, entitled “A Method forPreparing Nanoparticle Compositions with Amphiphilic Copolymers,” theentirety of which is incorporated by reference herein.

FIELD OF THE INVENTION

The present invention relates to processes and apparatuses for preparingcompositions of small particles from amphiphilic copolymers, oftensmaller than 100 nm, capable of maintaining sufficient stability forpost processing or for trnsporting or targeting an additive targetmolecule. These particles are referred to herein as “nanoparticles.”When these particles contain an additive target molecule, they are oftensmaller than 1060 nm in diameter. The process presents a means ofcontrolling the size of the particles and can be used to mix variousadditives with thenanoparticles for a wide range of uses.

BACKGROUND OF THE INVENTION

Nanoparticales can be used as micro-reactor vessels, to modify the flowproperties of materials, or for delivery of pharmaceutical, cosmetic oragricultural agents. In addition, formation of nanoparticles withpolymers has been used in various industries to modify the miscible andvolatile properties of target molecules. For instance, nanoparticles canbe used to create a drug delivery system for therapeutic agents that arehydrophobic in nature and cannot be administered either orally orthrough intravenous injection because they are not water-soluble. Suchtherapeutic agents can be incorporated into nanoparticles dispersed inan aqueous solution resulting in a composition that is suitable forinjection, inhalation, or oral administration. In addition, theparticles can be made small enough for filtration purification and toassure that the nanoparticles will not clog capillaries or alveoli.Also, smaller particles can enhance transfer rates to the body orfoliage due to the associated increase in the surface area per volume.

Some polymers have been found to be mucoadherents or have been shown tobind preferentially to mucosal linings in vitro. One such polymercontains polyacrylic acid (“PAA”), which is considered an appropriatevehicle for oral administration because when presented on the surface ofa nanoparticle it demonstrates adherence to the gastrointestinal tractand can improve drug delivery in the lower intestinal tract. PAA alsodemonstrates a high non-covalent affinity for vaginal mucosal lining.Mucoadhesive properties in a drug coating can be used to target a highlypotent or water insoluble drugs to a targeted area in the patient. Bytargeting the drug to amucosal lining, a lower dose may be administeredwith the same therapeutic effect. In addition, an altered watersolubility of a drug should increase its bioavailability.

Additional polymers that are mucoadherents and are potential componentsin pharmaceutical formulations include poly(d-glucosamine),poly(d-glucaronic acid-N-acetylglucosamine),poly(N-isopropylacrylamide), poly(vinyl amine), and poly(methacrylicacid). “Mucoadhesion of polystyrene nanoparticles having surfacehydrophilic polymeric chains in the gastrointestinal tract”International Journal of Pharmaceutics 177 (1999) 161-172. “BioadhesionTechnologies for the delivery of Peptide and Protein Drugs to theGastrointestinal Tract” Critical Reviews in Thereapeutic Drug CarrierSystems 11(2&3):119-160 (1994). “pH-Dependant Dissolving Nano- andMicroparticles for improved Peroral Delivery of a Highly LipophilicCompound in Dogs” AAPS PharmSci 2001; 3 (1) article 8.

Polyethylene oxide (“PEO”) is another desirable compound for use inpharmaceutical compositions. For example, hiposomes with PEO on theexterior surface have been shown useful to prolong blood circulationlifetimes, decrease the rate of uptake into the mononuclear phagocytesystem, and allow crossing in vivo biological barriers. PEO liposomesalso have been shown to decrease the toxicity and increase the stabilityof an administered drug. “Interaction of PEG-Phospholipid Conjugateswith phospholipid implication in the Liposomal Drug Delivery,” AdvancedDrug Delivery Reviews, 16:235-247 (1995). “Long Circulating (stericallystabilized) Liposomes for targeted drug delivery,” TiPS 15:215-220(1994).

The formation of nanoparticles has been achieved by various methods.Nanoparticles can be made by precipitating a molecule in awater-miscible solvent, and then drying and pulverizing the precipitateto form nanoparticles. (U.S. Pat. No. 4,726,955). Similar techniques forpreparing nanoparticles for pharmaceutical preparations include wetgrinding or milling. Other methods include mixing low concentrations ofpolymers dissolved in a water-miscible solution with an aqueous phase toalter the local charge of the solvent and form a precipitate throughconventional mixing techniques. (U.S. Pat. No. 5,766,635). Other methodsinclude the mixing of copolymers in organic solution with an aqueousphase containing a colloid protective agent or a surfactant for reducingsurface tension. Other methods of incorporating additive therapeuticagents into nanoparticles for drug delivery require that nanoparticlesbe treated with a liposome or surfactant before drug administration(U.S. Pat. No. 6,117,454).

Typically, current methods for forming nanoparticles by precipitationdemonstrate little or no control of particle size and show poor yields.Uncontrolled and unpredictable particle size is particularlydisadvantageous in the formation of pharmaceutical and agriculturalproducts. Furthermore, large scale production of nanoparticles usingestablished methods can be quite costly due to the low concentration ofpolymer initially introduced into the process solvent prior tonanoparticle production. Finally, many production techniques such asmiling or wet grinding introduce the possibility of contamination intothe final product.

In addition, methods for forming nanoparticles with additive targetmolecules contained within the nanoparticle typically have beenperformed with additives at very low ratios compared with copolymer andat low absolute concentration. Therefore, the fraction of additivetarget molecule per nanoparticle is minimal, and the cost of productionis high. Lowering the ratio of copolymer to additive target molecule isdesirable to increase the number of resulting nanoparticles that containadditive target molecule and the amount of additive target moleculescontained within the nanoparticles as well as reduce the amount ofinitial copolymer needed to create these nanoparticles.

For the foregoing reasons, there is a need for a process of creatingnanoparticles with copolymers in which the size of the resultingnanoparticle can be predicted and controlled, additives can beincorporated into the nanoparticle at a high yield, and the amount ofcopolymer initially needed is reduced. Furthermore, there is a long feltneed for a process of producing nanoparticles at a high concentrationand in which the nanoparticles produced can be harvested easily and witha high yield.

SUMMARY OF THE INVENTION

The present invention is directed to a process and apparatuses forcarrying out that process in which nanoparticles are created fromamphiphilic copolymers at a predictable and controlled size and yield.The formation of nanoparticles is induced by mixing at least one processsolvent comprising amphiphilic copolymers with at least one non-processsolvent capable of changing the charge of the local molecularenvironment of the amphiphilic copolymers. Optionally, the processsolvent(s) or non-process solvent(s) can contain an additive targetmolecule useful for a specific indication which can be coprecipitated orcoated with the amphiphilic copolymer. The process solvent ornon-process solvent can also contain supplemental additives useful forthe production or subsequent use of the nanoparticles.

The apparatuses for carrying out the processes disclosed herein use acontrolled mixing velocity in either a batch or continuous configurationfor introduction of the process solvent and non-process solvent streams.The introduction of the process streams into these mixers allows a“flash” precipitation to occur yielding nanoparticles. The nanoparticlesproduced exhibit sufficient stability for post processing for use inpharmaceutical, medical, or agricultural applications.

The process of mixing molecules of initially separate fluids tohomogeneity is called “micromixing.” The time to achieve homogeneity isidentified by the characteristicmicromixing time τ_(m), or simply themixing time. Copolymer precipitation occurs in a finite time, which isidentified as τ_(agg) and the characteristic time for target molecule,an organic active, precipitation is designated as τ_(ng). The mixingtime is controlled by the physical operation of the mixer and theprecipitation times are controlled by the initial choices ofcompositions and conditions for mixing and the compositions existing andconditions at the molecular level during the mixing process.

The ratio of each of these times can effect the size and yield of themicro- or nanoparticles produced. Marcant and David have shown the rateat which the two fluids are micromixed can control the resultingparticles sizes in precipitation. Marcant and David.Experimental-Evidence for and Prediction of Micromrxing Effects inPrecipitation. AIChE Journal 37(11): 1698-1710 (1991). In the case ofnanoparticles, the same principles can apply, but due to the very smallsize of nanoparticles, the process occurs very fast, essentially in a“flash.” A mixer that is sufficiently fast to reduce the mixing time,τ_(m), of the fluids to below the precipitation times, τ_(agg) andτ_(ng), can critically effect the process.

In the present invention, micromixing is achieved by using either acontinuous flash mixer or a batch flash mixer. The flow rate,temperature, and pressure of each stream entering or in the mixer can becontrolled. Additionally, a centripetal mixer can be used for flashprecipitation of nanoparticles from amphiphilic copolymers.

In a continuous flash mixer at least one process solvent and at leastone non-process solvent are continually added to a mixing vessel throughinlet tubes. The resulting mixture is removed from the mixer for aperiod of time under a steady state condition. In one embodiment, theprocess solvent(s) and a non-process solvent(s) are introduced into amixing vessel through separate inlet tubes. The tubes are introduced ina confined region where intimate mixing of the stream can occur rapidlyand locally mix in the ratio they were charged. The confined region isenclosed and beneficial to enhancing the mixing. In another embodimentthe confined region is open and the streams are directed substantiallytowards one another to facilitate rapid or controlled mixing or are inthe presence of a mechanical agitator to facilitate rapid or controlledmixing.

In a batch flash mixer, the non-process solvent is placed in a mixingvessel. The process solvent(s) and any additional non-process solvent(s)are introduced into a mixing vessel containing the non-process solventthrough at least one inlet tube at a controlled flow rate andtemperature. In a batch flash mixer, the process is not at steady stateand the contents of the mixer are continually changing as solventstream(s) is added to the batch. The batch is completed after thesolvent streams have been added. In one embodiment, the added solventstream(s) is introduced in a region near a mechanical agitator, wherethe mixing velocity is the greatest or is most easily controlled. Thispoint of introduction could also be a confined portion of the mixingvessel, such as in a recycle loop. An agitator is not required if thefluids added into the non-solvent have a high mixing velocity sufficientto mix the fluid contents rapidly and in a controlled fashion.

Nanoparticles can be formed by dissolving an amphiphilic copolymer in aprocess solvent at a concentration of at least 0.1% by weight, butpreferably the concentration of copolymer is at least 0.2% by weight.Examples of amphiphilic copolymers include but are not limited to blockcopolymers, graft copolymers, and random copolymers that include bothhydrophobic and hydrophilic regions within the same copolymer. Theprocess solvent includes, but is not limited to, alcohols and ethers.The process solvent can be heated or pressurized or both to facilitatedissolution of the amphiphilic copolymer, depending on the dissolutioncharacteristics of the copolymer in the solvent. Upon micromixing theprocess solvent containing the amphiphilic copolymer with a non-processsolvent, the amphiphilic character of the copolymer becomes apparent andeither the hydrophobic portion or the hydrophilic portion of thecopolymer can no longer exist in the soluble state, and thusprecipitates. The soluble portion of the amphiphilic copolymer affordssteric or steric and electrostatic stabilization of the nanoparticlessufficient for post processing or harvesting.

In one embodiment of the present invention, additive target moleculescan be added to the amphiphilic copolymer in the process solvent. Uponcreation ofnanoparticles with the amphiphilic copolymer, the additivetarget molecules will be incorporated in the nanoparticle. Additivetarget molecules that are poorly soluble in the non-process solvent arecoprecipitated, coated, encapsulated, or confined as a particulate coreand stabilized by the amphiphilic copolymer. The nanoparticles maintaina small and stable size for a time sufficient for post processing. Theadditive target molecules can be organic actives useful for apharmaceutical indication and poorly soluble in aqueous systems.Amphiphilic copolymers and the additive target molecules can be mixed ina ratio between about 1:20 to about 20:1 by weight and result innanoparticles of amphiphilic copolymers with additive target molecule.

In another embodiment of the invention, supplemental additives such ascolloidal-dispersants or surfactants can be included in the finalcolloid mixture to enhance the resultant properties of thenanoparticles, such as stabilization the nanoparticles.

The flash precipitation process and the associated flash mixingapparatuses described herein are useful for the production ofamphiphilic copolymer nanoparticle compositions including optionaladditive target molecules. With the processs and apparatuses describedherein, nanoparticles compositions can be made with a high content oftarget molecule with high yield, high productivity, and high processingrates while using low amounts of amphiphilic copolymers. Thenanoparticles compositions and processs described can be used for avariety of purposes including creating pharmaceutical, medical, andagricultural formulations and particle surface functionalization.

These and other features, aspects, and advantages of the presentinvention will become better understood with reference to the followingdescriptions and appended claims.

BRIEF DESCRIPTION OF THE DRAWINGS

The following Figures are included in this application to exemplify anddescribe the invention but are not intended to limit the embodiments ofthe invention.

FIG. 1 is a schematic drawing of a continuous flash mixer, presentingtwo inlets to a conical-domed mixing vessel with a conical outlet, avariety of outlet shapes are also presented including a conical, squareand mixed shape outlets at two different opening sizes;

FIG. 2 is a schematic drawing of a batch flash mixer in which the mixingmechanism is shown with a preferable position for the end of the inlettube in relation to the mixing or agitating device;

FIG. 3 is a graphic depiction of nanoparticle size in relation to themixing velocity for nanoparticles formed frompolystyrene(1000)-block-polyethyleneoxide(3000) (“PS(1000)-b-PEO(3000)”)in tetrahydrofuran (“THF”) and water in a continuous flash mixer. Theratios of mix time and aggregation time are also presented in relationto nanoparticle size;

FIG. 4 is a graphic depiction of volume percentage of nanoparticles bythe distribution of nanoparticle size for nanoparticles formed fromPS(1000)-b-PEO(3000) in THF and water in a continuous flash mixer andcontaining the additive target molecule, β-carotene, in a 1:1 ratio withcopolymer where copolymer and additive were both 2.6 wt %;

FIG. 5 is a graphic depiction of volume percentage of nanoparticles bythe distribution of nanoparticle size for nanoparticles formed fromPS(1000)-b-PEO(3000) in THF and water in a continuous flash mixer andcontaining the additive target molecule, β-carotene, in a 1:1 ratio withcopolymer after removal of organic solvent where copolymer and additivewere both 2.6 wt %;

FIG. 6 is a graphic depiction of volume percentage of nanoparticles inrelation to mean velocity and agitator tip speed for nanoparticlesformed from PS(1000)-b-PEO(3000) in THF and water in a batch flash mixerand containing the additive target molecule, β-carotene, in a 6.5:1ratio with copolymer;

FIG. 7 is a graphic depiction of mean nanoparticle size in relation tothe jet velocity for nanoparticles formed from PS(1000)-b-PEO(3000) inTHF and water in a continuous flash mixer and containing the additivetarget molecule, β-carotene, in a 6.5:1 ratio with copolymer;

FIG. 8 is a graphic depiction of nanoparticle size in relation to themixing velocity for nanoparticles formed frompolybutylacrylate(7500)-b-polyacrylicacid(7500)(“PBA(7500)-b-PAA(7500)”) in methanol (“MeOH”) and MeOH/water in acontinuous flash mixer for samples with having volume % MeOH of 83% and56% in the initial mixture;

FIG. 9 is a graphic depiction of nanoparticle size in relation to themixing velocity for nanoparticles formed from PBA(7500)-b-PAA(7500) atvarying weight percentage (wt %) concentration of copolymer beforemixing in MeOH and water in a continuous flash mixer; threshold mixingtimes and aggregation times are also presented in relation tonanoparticle size; and

FIG. 10 is a schematic diagram of a centripetal flash mixer with mixvelocities and nanoparticle production by volume percentage.

DETAILED DESCRIPTION OF THE INVENTION

The present invention relates to a process and apparatuses preparingnanoparticles from amphiphilic copolymers. The size of the resultingnanoparticles can be controlled by controlling the mixing velocity usedto create them. Nanoparticles can be produced from amphiphiliccopolymers that are dissolved in a process solvent. After theamphiphilic copolymers are dissolved in the process solvent, thesolution is rapidly mixed with a non-process solvent and nanoparticlesare flash precipitated in the resulting solution. This mixing can beachieved through various methods during which the mixing velocity iscontrolled. In addition, an additive target molecule can be mixed withthe amphiphilic copolymer in the process solvent prior to flashprecipitation for incorporation into the resulting nanoparticles.

In the present invention, mixing apparatuses are presented that arecapable ofreaching a critical and robust processing condition or a veryfast mixing velocity and capable of controlling the size of thenanoparticles, by controlling mixing time (“τ_(m)”) through control ofthe mixing velocity. The types of mixing apparatuses presented include acontinuous flash mixer and a batch flash mixer. Mixing velocity iscritical to controlling the nanoparticle size distribution, however,quantifying the actual τ_(m) is difficult. Therefore, it is practical touse the mixing velocity as an indicator of mixing time. For the examplespresented below that were performed using a continuous flash mixer, themixing velocity was considered to be the highest average velocity of anyof the fluids entering the mixing vessel. For the examples presentedthat were performed in a batch flash mixer, mixing velocity wasconsidered to be the greater of either the moving surface velocitycreated by the tip speed or the average velocity of the incoming fluid.Actual mixing velocities may have been higher or lower than theestimated mixing velocity of a single solvent stream or mix speed due tothe cumulative effect of two fluids or moving surfaces coming together.

A process solvent is a composition comprised of one or more fluidcomponents and capable of carrying a solid or solids in solution orsuspension. The process solvent is able to substantially dissolve theamphiphilic copolymer to a molecularly soluble state. A non-processsolvent is any composition that is substantially soluble with theprocess solvent and leads to the precipitation of the dissolved orsuspended amphiphilic copolymer after mixing with the process solvent.Precipitation of the amphiphilic copolymer upon mixing can be the resultof changes in temperature, composition, or pressure or any combinationof each. The process stream and non-process stream refer to the processand non-process solvents with the optional additive target molecules orsupplemental additives, respectively as they enter the mixer.

Flash Mixers

An example of a continuous flash mixer is shown in FIG. 1. Two solventstreams of fluid are introduced into a mixing vessel through independentinlet tubes having a diameter, d, which can be between about 0.25 mm toabout 6 mm but are between about 0.5 mm to about 1.5 mm in diameter forlaboratory scale production. The continuous flash mixer includestemperature controlling elements for fluid in the inlet tubes and in themixing vessel. In one embodiment, the inlet tubes are coiled in a waterbath that controls the temperature of the fluids passing through thetubes and the mixing vessel is placed in a water bath. In addition, themixing vessel contains a device to control and regulate the pressure ofits contents. In one embodiment of the invention, the solvent streamsare impacted upon each other while being fed at a constant rate from theinlet tube into the mixing vessel. In another embodiment of theinvention, more than two inlet tubes direct solvent streams into themixing vessel.

In one embodiment, the mixing vessel is a cylindrical chamber with ahemispherical top. The diameter of the mixing vessel, D, is typicallybetween 1.25 mm to about 30.0 mm but preferably is between about 2.4 mmto about 4.8 mm, and D/d is about 3 to 20. The mixing vessel alsocontains an outlet with a diameter, δ, that can be between about 0.5 mmto about 2.5 mm but is preferably between 1.0 mm to about 2.0 mm, andδ/d is about 1 to 5. In one embodiment, the outlet can be conical, inanother embodiment it can be square, and in another it can have a mixedconfiguration.

For the continuous flash mixer shown in FIG. 1, the mixing velocity isconsidered the highest average velocity of any of the fluid streamsentering the mixing vessel. If the interior of the mixing vessel is madelarge, D/d >40, the inlet tubes delivering the fluids to be mixed canprotrude into the interior of the vessel to direct fluid impact withinthe vessel and to ensure rapid mixing.

The mixing velocity is considered the highest average velocity of any ofthe fluid streams entering the mixing chamber. In one embodiment of theinvention, the angle of incidence of the two streams can be varied. Theangling of the inlet streams can affect the mixing velocity. Forexample, in one embodiment of the invention, the streams are directedtowards each other causing them to collide and essentially increasingthe mixing velocity while decreasing the mixing time. In one embodiment,the velocity of the fluid exiting the inlet tube is between about 0.02m/s and 12.0 m/s.

In one embodiment, the mixing vessel is a continuous centripetal mixer.In this embodiment, the process and non-process streams are directedinto a mixing vessel but do not directly impinge. The streams are forcedto the walls of the mixing vessel by centripetal forces. In anotherembodiment, the mixing vessel could be another high mixing velocity orhighly confined mixer such as, but not limited to, a static mixer, rotorstator mixer, or a centripetal pump where the process solvent isintroduced into the region of high mixing velocity. To those sillded inthe art, any mixer capable of providing a sufficient mixing velocitywith controlled introduction of the process streams could afford a flashprecipitation under the teachings of this disclosure.

In another embodiment of the invention, the dimensions of the continuousflash mixer can be scaled up to achieve desired production rates. Inthis embodiment, the process is performed at a steady state with thestreams continually introducing the desired composition ratio andcontinually draining from the mixing vessel. The effluent can becollected in a second holding tank, optionally with a liquid phasewithin, for further post processing.

In another embodiment of the invention, the process and non-processsolvents are mixed in a batch flash mixer. An example of a batch flashmixer is presented in FIG. 2. In this design, the process solvent streamcontaining the amphiphilic copolymer and the optional additive targetmolecule are added via an inlet tube to a non-process solvent in amixing vessel that has a mechanical agitator. The batch flash mixerincludes temperature controlling elements for fluids in the inlet tubesand mixing vessel. In one embodiment, the inlet tube is coiled in awater bath that controls the temperature of the fluid passing throughthe tube and the mixing vessel is submerged in a water bath. Inaddition, the mixing vessel contains a device to control and regulatethe pressure of its contents.

Fluid is introduced via an inlet tube into the region of high mixingintensity, near the sweep region of the mechanical agitator. In apreferred embodiment, a marine agitator with a single baffle is used inthe batch flash mixer, but other agitators or baffle configurationscould be employed. The placement of the incoming solvent stream can bevaried by varying the position of the inlet tube, but the fluid exitingthe inlet tube is usually fed directly into the region of high mixingintensity. The distance between the end of the inlet tube and theagitator tip is preferably within 15% of the agitator diameter of thecircular sweep made by the agitator. This ratio facilitates rapidincorporation of the incoming fluid into the swept region of themechanical agitator or rapid mixing with the immediate outflow of themechanical agitator. In one embodiment, the velocity of the fluidexiting the inlet tube is between about 0.02 m/s and 12.0 m/s. Inanother embodiment, the surface velocity of the fluid in the mixingvessel is between about 0.02 m/s and 8.5 m/s.

In one embodiment of the invention, the batch flash mixer includesmultiple inlet tubes for the introduction of more than one solventstream. In one embodiment of the invention, amphiphilic copolymer andadditive target molecule are introduced into the mixing vessel viadifferent solvent streams. In another embodiment, the fluid streams canbe directed towards each other to substantially cause them to collideand mix. In another embodiment of the invention, the dimensions of thebatch flash mixer can be scaled up to achieve desired production rateswith limited scale up of the inlet tube diameter relative to theagitator.

For the examples provided below in which a continuous flash mixer wasused, a constant flow rate was provided by a syringe pump for each inlettube using a Harvard Apparatus (model number 7023). At least one 100 mLglass syringe (SGE Inc.) was connected to each side of the mixer inFIG. 1. For each side of the mixers, the fluid to be mixed flowed fromthe syringe pumps into a coil of ⅛^(th)-inch stainless steel through anarrowing tube and into the mixing vessel. The ⅛^(th)-inch coil and thecontinuous flash mixer were submerged in a temperature bath to controlthe temperature of the fluid entering the continuous flash mixer. Theoutlet of the mixer was connected to an 8-inch line of ⅛^(th)-inchtubing leading out of the temperature bath for product collection.

For the examples provided below in which a continuous flash mixer wasused, a constant flow rate was provided by a syringe pump for each inlettube using a Harvard Apparatus (model number 7023). At least one 100 nLglass syringe (SGE Inc.) was connected to each side of the mixer inFIG. 1. For each side of the mixer, the fluid to be mixed flowed fromthe syringe pumps into a coil of ⅛^(th)-inch stainless steel through anarrowing tube and into the mixing vessel. The ⅛^(th)-inch coil and thecontinuous flash mixer were submerged in a temperature bath to controlthe temperature of the fluid entering the continuous flash mixer. Theoutlet of the mixer was connected to an 8-inch line of ⅛^(th)-inchtubing leading out of the temperature bath for product collection.

For the examples presenting a batch flash mixer, the process solvent wasinjected through an inlet tube at a constant flow rate by a syringe pump(model number 7023, Harvard Apparatus) comprising at least one 100 mLglass syringe (SGE, Inc.) into the mixing vessel containing thenon-process solvent. The stream flowed from the syringe pump and into acoil of ⅛^(th)-inch stainless steel through a narrowing device into a1.0 mm-tube and into the mixing vessel. The ⅛^(th)-inch coil wassubmerged in a temperature bath to control the temperature of the fluidentering the batch flash mixer. The temperature of the contents of thebatch flash mixer can be varied using conventional means including hotplates and water baths.

In the case of the centripetal mixer, the non-solvent was supplied usinga pressurized vessel and the flow rate was controlled by adjusting thepressure of the vessel or using a control valve. A Harvard Apparatuswith a 100 mL syringe was also used with this mixer.

Amphiphilic Copolymers

Amphiphilic copolymers are comprised of sub-units or monomers that havedifferent hydrophilic and hydrophobic characteristics. Typically, thesesub-units are present in groups of at least two, comprising a block of agiven character, such as a hydrophobic or hydrophilic block. Dependingon the method of synthesis, these blocks could be of all the samemonomer or contain different monomer units dispersed throughout theblock, but still yielding blocks of the copolymer with substantiallyhydrophilic and hydrophobic portions. These blocks can be arranged intoa series of two blocks (diblock) or three blocks (triblock), or more,forming the backbone of a block copolymer. In addition, the polymerchain can have chemical moieties covalently attached or grafted to thebackbone. Such polymers are graft polymers. Block units making up thecopolymer can occur in regular intervals or they can occur randomlymaking a random copolymer. In addition, grafted side chains can occur atregular intervals along the polymer backbone or randomly making arandomly grafted copolymer. The amphiphilic copolymers used in thisinvention are comprised of blocks of at least two sub-units or with aminimum contour length the equivalent of at least 5 ethylene units andof a given character and a molecular weight of at least 300 g/mole.Contour lengths are the linear sum of the polymer backbone, themolecular dimensions of which can be approximated using the PolymerHandbook, 4^(th) Edition, eds. S. Brandrup, E. H. Immergut, and E. A.Grulke, assoc. ed. A. Abe, D. R. Bloch, 1999, New York, John Wiley &Sons, the disclosure of which is hereby incorporated by reference in itsentirety.

Amphiphilic copolymers could also contain a polymeric block or blocks asgiven herein connected to a moiety of considerable size that is not apolymeric chain consisting of sub units. In this case the molecularweight of the moiety is greater than 300 g/mole. It is often preferableto have the moiety be at least 1000 g/mole to enhance the post mixingsoluble or non-soluble character of the moiety.

Amphiphilic copolymers possess both hydrophobic and hydrophilic regionsalong the same polymer chain. Hydrophobic and hydrophilic regions maybecomprised of blocks of polymer or may have theirhydrophilicity/hydrophobicity affected by a grafted moiety. The uniquecharacteristics of an amphiphilic copolymer allows the copolymer toprecipitate locally when its solvent conditions are changed. Forinstance, an amphiphilic copolymer dissolved in a charge-neutral solventshould locally precipitate when mixed with charged solvent causing thehydrophilic regions to take a conformation maximizing contact with thecharged solvent and the hydrophobic regions to minimize contact with itor locally precipitate. Preferably, the hydrophilic block should be atleast 1000 g/mole to facilitate colloidal stability via steric or stericand electrostatic means after nanoparticle formation. Preferably, thehydrophobic block is of at least 1000 g/mole to enhance the non solublecharacter of the block and promote precipitation.

Nanoparticles formed by the process of this invention can be formed withgraft, block or random amphiphilic copolymers. These copolymers can havea relatively low molecular weight, between 1000 g/mole and 50,000g/mole, or preferably between about 3000 g/mole to about 25,000 g/mole,and more preferably at least 2000 g/mole. Alternatively, the amphiphiliccopolymers used in this invention exhibit a surface tension whendissolved in water at 0.1 wt % of at least 50 dynes/cm.

Examples of suitable hydrophobic sub-units that comprise hydrophobicblocks in an amphiphilic copolymer include but are not limited to thefollowing: acrylates including methyl acrylate, ethyl acrylate, propylacrylate, n-butyl acrylate (“BA”), isobutyl acrylate, 2-ethyl acrylate,and t-butyl acrylate; methacrylates including ethyl methacrylate,n-butyl methacrylate, and isobutyl methacrylate; acrylonitriles;methacrylonitrile; vinyls including vinyl acetate, vinylversatate,vinylpropionate, vinylformamide, vinylacetamide, vinylpyridines, andvinyllimidazole; aminoalkyls including aminoalkylacrylates,aminoalkylsmethacrylates, and aminoalkyl(meth)acrylamides; styrenes; andlactic acids. Examples of suitable hydrophilic sub-units in anamphiphilic copolymer include but are not limited to the following:carboxylic acids including acrylic acid, methacrylic acid, itaconicacid, and maleic acid; polyoxyethylenes or polyethyleneoxide; andunsaturated ethylenic mono or dicarboxylic acids. Preferably the blocksare either diblock or triblock in nature. Preferably, block copolymersfor this invention include blocks substantially comprising the monomersof polystyrene, polyethylene, polybutyl acrylate, polybutylmethacrylate, polylactic acid, polyacrylic acid, polyoxyethylene orthose that are biocompatible. Additional preferable polymers shown to bemucoadherents and preferable for incorporation into amphiphiliccopolymers include, but are not limed to, monomers of poly (acrylicacid), poly(d-glucosamine), poly(d-glucaronic acid-N-acetylglucosamine),poly(N-isopropylacrylamide), poly(vinyl amine), and poly(methacrylicacid).

In graft copolymers, the length of a grafted moiety can vary.Preferably, the grafted segments are alkyl chains of 4 to 18 carbons orequivalent to 2 to 9 ethylene units in length. In addition, the graftingof the polymer backbone can be useful to enhance solvation ornanoparticle stabilization properties. A grafted butyl group on thehydrophobic backbone of a diblock copolymer of a polyethylene andpolyethylene glycol should increases the solubility of the polyethyleneblock. Suitable chemical moieties grafted to the block unit of thecopolymer comprise alkyl chains containing species such as, but notlimited, to amides, imides, phenyl, carboxy, aldehyde or alcohol groups.

The amphiphilic copolymer can be selected from several groups ofcopolymers including polystyrenes, polyethyleneglycols, polyglutamicacids, hyaluronic acids, polyvinylpyrrolidones, polylysines,polyarginines, alginic acids, polylactides, polyethyleneimines,polyionenes, polyacrylic acids, and polyiminocarboxylates. Anybiocompatable amphiphilic copolymer can be used. Preferably, theamphiphilic copolymer is comprised of diblock or triblock compositionscontaining at least one of the following: a polystyrene block, apolyethylene oxide block, a polybutylacrylate, a polyacrylic acid,polybutylmethacrylate block, or a polyethyleneoxide block.

Additive Target Molecules

The amphiphilic copolymer is dissolved in a process solvent capable ofdissolving at least 0.1% of the copolymer by weight and that istypically a liquid at room temperature. In one embodiment of theinvention, the process solvent is a mixture of solvents or an organicsolvent. In a more preferred embodiment of the invention, the processsolvent is an alcohol or ether. In another embodiment, the processsolvent is methanol. In yet another embodiment, the process solvent istetrathydrofuran (“THF”). The concentration of the amphiphilic copolymerin the process solvent may be increased by controlling the temperatureand the pressure of the mixture. In the present case, nanoparticlecompositions in which amphiphilic copolymers contain PEO as the watersoluble component are used for steric stabilization of a target moleculeare desirable to obtain the properties for a pharmaceutical formulation.If linked to a hydrophobic species or polymer chain, the amphiphiliccopolymer can be used to coat hydrophobic target molecules where theexterior of the particles presents PEO as soluble in an aqueous phase.

In another embodiment of the invention, the process or non-processsolvent may consist of a liquefied gas. In this embodiment, the processor non-process solvents are a gas at room temperature but are put inliquid form for the process by changing the pressure or temperature orboth in the mixing vessel or inlet tubes. An example of a liquefied gasused as a non-process solvent is carbon dioxide under adequate pressurewith or without a modifier, such as ethanol. After mixing, a postprocessing step consisting of a pressure or temperature change or achange in both is made and the solvent evaporates leaving thenanoparticles.

In another embodiment of the invention, nanoparticles are made andinclude an additive target molecule. In one embodiment, an additivetarget molecule is mixed with theamphiphilic copolymer in the processsolvent phase. In another embodiment the additive is combined with theamphiphilic copolymer in a ratio of 1:4 to 10:1 by weight or charge. Instill another embodiment, the additive target molecule is mixed with theamphiphilic copolymer in at least a 1:2 ratio by weight. Preferably thetarget molecules is present in the process solvent streams after mixingat a concentration of at least 0.1% by weight, but more preferably theconcentration of target molecule is at least 0.2% by weight. Thetemperature and the pressure of the process solvent can be altered toallow complete dissolution of both the amphiphilic copolymer and theadditive target molecule while maintaining a liquid phase. One suchsolvent would be ethanol and the mixing process is performed at elevatedpressure.

Examples of some preferred additive target molecules that may be addedtonanoparticles by this process can be selected from the known classesof drugs including immunosuppressive agents such as cyclosporins(cyclosporin A), immunoactive agents, analgesics, anti-inflammatoryagents, anthelmintics, anti-arrhythmic agents, antibiotics (includingpenicillins), anticoagulants, antidepressants, antidiabetic agents,antiepileptics, antihistamines, antihypertensive agents, antimuscarinicagents, antimycobacterial agents, antineoplastic agents,immimosuppressants, antithyroid agents, antiviral agents, anxiolyticsedatives (hypnotics and neuroleptics), astringents, beta-adrenoceptorblocldng agents, blood products and substitutes, cardiac inotropicagents, contrast media, corticosteroids, cough suppressants(expectorants and mucolytics), diagnostic agents, diagnostic imagingagents, diuretics, dopaminergics (antiparkinsonian agents),haemostatics, immuriological agents, lipid regulating agents, musclerelaxants, parasympathomimetics, parathyroid calcitonin andbiphosphonates, prostaglandins, radio-pharmaceuticals, sex hormones(including steroids), anti-allergic agents, stimulants and anoretics,sympathomimetics, thyroid agents, vasodilators, xanthines,anti-oxidants, preservatives, vitamins, and nutrients. Preferred drugsubstances include those intended for oral administration andintravenous administration. They can be selected from any pharmaceuticalorganic active and precursor compound. A description of these classes ofdrugs and a listing of species within each class can be found inPhysicians Desk Reference, 51 edition, 2001, Medical Economics Co.,Montvale, N.J., the disclosure of which is hereby incorporated byreference in its entirety. The drug substances are commerciallyavailable and/or can be prepared by techniques known in the art. Otheradditive target molecules include agricultural compounds, biocides,pesticides, herbicides, fungicides, and insecticides.

In a preferred embodiment, the additive target molecule is an organicactive compound that is co-precipitated with the amphiphilic copolymer.The target molecule should be substantially insoluble in solutioncreated after the mixing process is complete. The target molecule istypically supersaturated or above its solubility during the mixingprocess and precipitates in a characteristic time τ_(ng). In a morepreferable embodiment, the target molecule is poorly soluble in water, 1wt %, and more preferably <0.1 wt %, at a specific pH. In this case, thetarget molecule is molecularly soluble in one of the process streamsprior to the flash precipitation.

In one embodiment, the target molecule is an anti-oxodant or aprovitamin of poor water solubility, <0.1 wt %. For instance, the targetmolecule could be β-carotene. The amphiphilic copolymer contains ahighly hydrophobic block and a hydrophilic block. The hydrophilic blockmight include a polystyrene-block-polyethyleneoxide (“PEO”) block. Theprocess solvent is tetrahydrofuran (“THF”) and the non-process solventis water. In this case, PEO is presented to the outside of the moleculemaking the material dispersable in water.

Process and Non-Process Solvents

The solution of process solvent containing either amphiphilic copolymeralone or with an additive target molecule is mixed with a non-processsolvent. The non-process solvent must be capable of changing the localmolecular environment of the copolymer and cause local precipitation ofeither the hydrophobic or hydrophilic blocks. The non-process solventcan be water that is either distilled, filtered or purified by reverseosmosis (RO″) or an aqueous solution containing a buffering agent, salt,colloid dispersant, or inert molecule. The non-process solvent couldalso be a mixture of solvents, such as alcohol and water. Using flashprecipitationprocesss described herein, nanoparticles are formed in thefmal mixed solution. The final solvent containing thenanoparticles canbe altered by a number of post treatment processes, such as but notlimited to dialysis, distillation, wiped film evaporation,centrifugation, lyophilization, filtration, sterile filtration,extraction, supercritical fluid extraction, or spray drying. Theprocesses typically occur after the nanoparticle formation but couldalso occur during the nanoparticle formation process.

Supplemental Additives

One or more supplemental additives can be added to the process solventor non-process solvent streams or to a stream of nanoparticles afterformation by flash precipitation to taylor the resultant properties ofthe nanoparticles or for use in a particular indication. Examples ofsupplemental additives include inert diluents, solubilizing agents,emulsifiers, suspending agents, adjuvants, wetting agents, sweetening,flavoring, and perfuing agents, isotonic agents, colloidal dispersantsand surfactants such as but not limited to a charged phospholipid suchas dimyristoyl phophatidyl glycerol; alginic acid, alignates, acacia,gum acacia, 1,3 butyleneglycol, benzalkonium chloride, collodial silicondioxide, cetostearyl alcohol, cetomacrogol emulsifying wax, casein,calcium stearate, cetyl pyridiniumn chloride, cetyl alcohol,cholesterol, calcium carbonate, Crodestas F-110®, which is a mixture ofsucrose stearate and sucrose distearate (of Croda Inc.), clays, kaolinand bentonite, derravitives of cellulose and their salts such ashydroxypropyl methylcellulose (HMPC), carboxymnethylcellose sodium,carboxymethylcellulose and its salts, hydroxypropyl celluloses,methylcellulose, hydroxyethylcellulose, hydroxypropylcellulose,hydroxypropylmethylcellulose phthalate, noncrystalline cellulose;dicalcium phosphate, dodecyl trimethyl aminonium bromide, dextran,dialkylesters of sodium sulfosuccinic (e.g. Aerosol OT® of AmericanCyanamid), gelatin, glycerol, glycerol monostearate, glucose,p-isononylphenoxypolt-(glycidol), also known as Olin 10-G® or surfactant10-G® (of Olin Chemicals, Stamford, Conn.); glucamides such asoctanoyl-N-methylglucamide, decanoyl-N-methylglucamide;heptanoyl-N-methylglucamide, lactose, lecithin(phosphatides), maltosidessuch as n-dodecyl β-D-maltoside; mannitol, magnesium stearate, magnesiumaluminum silicate, oils such as cotton seed oil, corn germ oil, oliveoil, castor oil, and sesame oil; paraffin, potato starch, polyethyleneglycols (eg the Carbowaxs 3350® and 1450®, and Carbopol 9340® of UnionCarbide), polyoxyethylene alkyl ethers (eg. macrogol ethers such ascetomacrogol 1000), polyoxyethylene sorbitan fatty acid esters (eg. thecommercially available Tweens® of ICI specialty chemicals),polyoxyethylene castor oil derivatives, polyoxyethylene sterates,polyvinylalcohol(PVA), polyvinylpyrrolidone(PVP), phosphates,4(1,1,3,3-tetramethylbutyl) phenol polymer with ethylene oxide andformaldehyde, (also known astyloxapol, superione, and triton), allpoloxamers and polaxamines (e.g., Pluronics F68LF®, F87®, F108® andtetronic 908® available from BASF Corporation Mount Olive, N.J.),pyranosides such as n-hexyl β-D-glucopyranoside, n-heptylβ-D-glucopyranoside; n-octyl-β-D-glucopyranoside, n-decylβ-D-glucopyranoside; n-decyl β-D-maltopyranoside; n-dodecylβ-D-glucopyranoside; quaternary ammonium compounds, silicic acid, sodiumcitrate, starches, sorbitan esters, sodium carbonate, solid polyethyleneglycols, sodium dodecyl sulfate, sodium lauryl sulfate (e.g., Duponol P®of DuPont corporation), steric acid, sucrose, tapioca starch, talc,thioglucosides such as n-heptyl β-D-thioglucoside, tragacanth,triethanolamine, Triton X-200® which is a alkyl aryl polyether sulfonate(of Rhom and Haas); and the like. The inert diluents, solubilizingagents, emulsifiers, adjuvants, wetting agents, isotonic agents,colloidal dispersants and surfactants are commercially available or canbe prepared by techniques know in the art. The properties of many ofthese and other pharmaceutical excipients suitable for addition to theprocess solvent streams before or after mixing are provided in Handbookof Pharmaceutical Excipients, 3rd edition, editor Arthur H. Kibbe, 2000,American Pharmaceutical Association, London, the disclosure of which ishereby incorporated by reference in its entirety.

Colloidal dispersants or surfactants can be added to colloidal mixturessuch as a solution containing nanoparticles to prevent aggregation ofthe particles. In one embodiment of the invention, a colloidaldispersant is added to either the process solvent or non-process solventprior to mixing. In one embodiment, the colloidal dispersant can includea gelatin, phospholipid or pluronic. The dispersant is typically addedin a ratio up to 2:1 with the additive target molecule by weight. Theuse of a colloidal dispersant can prevent nanoparticles from growing toa size that makes them useless.

In another embodiment of the invention, the additive target molecule ismixed with the amphiphilic copolymer with a supplemental seedingmolecule. The inclusion of a supplemental seed molecule in the processsolvent facilitates the creation ofnanoparticles upon micromixing withthe non-process solvent Examples of a supplemental seed moleculeinclude, but are not limited to, a substantially insoluble solidparticle, a salt, a fumctional surface modifier, a protein, a sugar, afatty acid, an organic or inorganic pharmaceutical excipient, apharmaceutically acceptable carrier, or a low molecular weight oligomer.

In one embodiment, a supplemental surfactant can be added to the processor non-process solvents. This process can be performed with amphiphiliccopolymer alone or with amphiphilic copolymers containing an additivetarget molecule.

Nanoparticles

Preferably the nanoparticle compositions containing one or moreamphiphilic copolymers, with or without one or more target molecules,and with or without one or more supplemental additives which areproduced by a flash precipitation of the invention have an average sizeless than 1060 nm and more preferably less than about 700 nm, less thanabout 500, less than about 400, less than about 200, less than about100, less than about 40 nm. The average size is on a weight basis and ismeasured by light scattering, microscopy, or other appropriate methods.Preferably at least 65% of the particles by weight have a particles sizeless than 1060 nm, and more preferably at least 80% of the particles areless than 1060 nm, and even more preferable at least 95% of theparticles on a weight basis have a particle size less than 1060 nm asmeasured by light scattering, microscopy, or other appropriate methods.

Processing of Nanoparticle Compositions

The nanoparticles produced by the flash precipitation process can bepost processed to yield a sterile aqueous or nonaqueous solution ordispersion or could be isolated, such as via lylophilization andautoclaving, to yield a sterile powders for reconstitution into sterileinjectible solutions or dispersions. The nanoparticles can be combinedwith other acceptable compounds for parenteral injection such as but notlimited to one or more of the following water, ethanol, propyleneglycol,polyethyleneglycol, glycerol, vegetable oils, ethyl oleate. Supplementaladditives suitable suitable for parenteral injection can also be used totaylor the composition to that suitable for a specific purpose.

In one embodiment, nanoparticles are formed in the absence of a targetmolecule. The hydrophobic additive target molecule and optionallysupplemental additives are added and the nanoparticles are loaded with atarget molecule using differential partitioning where the solventquality for the target molecule is slowly changed using dialysis ordistillation. The resulting loaded particles are then isolated and usedin a pharmaceutical formulation.

In one embodiment, the stream of nanoparticles produced via the flashprecipitation, is distilled to remove any toxic solvents and sterilefiltered using a 0.22 μm nominal pore size filter to yield a sterilesolution. In another embodiment, the process solvent streams aresterilized prior to use and are flash precipitated in a sterileenvironment to produce a sterile formulation. Any post processing isalso performed under sterile conditions.

The nanoparticulate compositions produced by the herein via flashprecipitation may also contain supplemental additives useful forpreserving, wetting, emulsifying, or dispensing the pharmaceuticalcomposition. Prevention of the growth of microorganisms can be ensuredby various antibacterial and antiftingal agents, such as but not limitedto sorbic acid, parabens, phenol, chlorobutanol. It may be desirable toadd an antioxidant such as tocopherol or it may be desirable to includeisotonic agents, such as sugars or sodium chloride.

In one embodiment, the nanoparticles formed via flash precipitation areisolated via distillation to remove toxic solvents such as THF, asupplemental additive is added, such as the cryoprotectant sucrose ortrehelose, and the material is lyophilized to obtain a powder.

In one embodiment, the nanoparticle compositions produced by a flashprecipitation of the invention are formulated into a solid dosage formfor oral administration such as capsules, tablets, pills, powders, andgranules. In such solid dosage forms, the nanoparticle composition isadmixed with one or more supplemental additives falling into thefollowing classes such as but not limited to lubricants, bufferingagents, wetting agents, adsorbtion, inert excipients, binders,disintegrating agents, solution retarders, accelerators, adsorbents, orfillers or extenders or other components commonly used by those skilledin the art for production of solid dosage forms.

In one embodiment, nanoparicles created by flash precipitation are madecomprising a exterior presenting a mucoadherent such as polyacrylic acidto the surface. Preferable that mucoadherent is part of apolybutylacrylate-b-polyacrylic acid amphiphilic copolymer. Theparticles are subsequently formulated as a delayed release methodcapable of presenting the mucoadherent to the lower gastrointestinaltract.

In one embodiment, the nanoparticle compositions is a potentpharmaceutical containing one or more amphiphilic copolymers, with orwithout one or more target molecules, and with or without one or moresupplemental additives which are produced by a flash precipitation ofthe invention are made into a solid dosage form and due to itsnanoparticulate size it is evenly dispersed throughout said solid dosageform admixture and yields a high content uniformity(quantity of materialin each dose) not obtained if the drug was microparticulate.

In one embodiment, the nanoparticle compositions produced by a flashprecipitation of the invention are formulated into a pharmaceuticallyacceptable liquid dosage form for oral administration such as a syrup,solution, emulsion, suspension, or elixir. In addition to theamphiphilic copolymer nanoparticulates, the liquid dosage forms maycomprise inert diluents, solubilizing agents, oils, emulsifiers,adjuvants suspending agents, sweeteners, wetting agents, flavoringagents, perfuming agents or other compounds commonly used by thoseskilled in the art.

The nanoparticle compositions containing one or more amphiphiliccopolymers, with or without one or more target molecules, and with orwithout one or more supplemental additives which are produced by a flashprecipitation of the invention can be administered to humans and animalsvia a number of means including but not limited to orally, rectally,parenterally (intravenous, intramuscular, or subcutaneous),intracisternally, intravaginally, intraperitoneally, locally (in theform of powders, ointments or drops) or as a buccal or nasal spray.

Particle Functionalization

In another embodiment of the invention, pre-existing nano- ormicroparticles can be functionalized by treatment with an amphiphiliccopolymer. In this embodiment, the pre-existing particle is dispersed ina solvent at a controlled temperature and pressure. An amphiphiliccopolymer is dissolved in a solvent capable of mixing with the solventcontaining the pre-existing particle but have different solubilitycharacteristics for the amphiphilic copolymer. The two solutions arethen mixed with a controlled temperature and mixing velocity causingselective precipitation of at least one amphilyte portion of theamphiphilic copolymer and at least one amphilyte portion of the samecopolymer remains soluble through flash precipitation of the amphiphiliccopolymer and the pre-existing particles. The resulting product containsparticles that have been functionalized by flash precipitation with anamphiphilic copolymer. Preferably, the average size of thefunctionalized particle is within 30% of its initial size. The initialsize of the particles can be <50 μm or over 2300 nm. In a preferredembodiment, the ratio of pre-existing particle to amphiphilic copolymeris 1:1. Pre-existing particles can be comprised of biologically ororganically active compounds or precursors, anti-inflammatories,anti-depressants, anti-oxidants, proteins, water insoluble vitamins,agricultural actives or precursors, ceramics, latex, glass, or metal.

EXAMPLES

Some illustrative but non-limiting examples are provided hereunder forthe better understanding of the present invention and for itsembodiments.

For the examples containing a substantial fraction of nanoparticles <100nm in diameter, photon correlation spectroscopy was performed on aBrookhaven with an ALV5000 multiple tau correlator to determine theaverage particle size using a second order cumulant fit. In accordancewith standard practice, the viscosity and index of refraction of thesolvent at a volume percentage the same as after mixing were input asproperties of the fluid. A Malvern Mastersizer S version 2.18 was alsoused to determine the particle size distribution based on volume, orsimilar to a weight. Likewise, the average particle size was based onvolume or mass, D[4,3]. The data analysis used a polydisperse model andthe Standard-Wet (3OHD) presentation that assumes the particle issuspended in water. Some samples were diluted with water for analysis.For all processing conditions, the water used was purified by RO andfiltered and the temperature is given within 2° C. The polymer blockswere nominal molecular weight with the nomenclature (1000) describing ablock nominally of 1000 g/mole. The blocks could have contained minorimpurities (<10% by weight and typically <5% by weight) due to themethod of synthesis.

Example 1 Nanoparticles of Polystyrene-block-polyethyleneoxide(“PS(1000)-b-PEO(3000”) in Tetrahydrofuran (“THF”) and Water Made in aContinuous Flash Mixer

This example demonstrates the ability of the continuous flash mixer toproduce nanoparticles that are <100 nm in diameter by controlling themixing.

A total of 0.71 grams of an amphiphilic block copolymer,PS(1000)-b-PEO(3000), was dissolved in 152 grams of tetrahydrofuran(“THF”) and 48.4 grams of RO purified water. This mixture'sconcentration was 0.35 weight percent (“wt %”) amphiphilic copolymer inTHF containing 20 volume percent (“volume %”) water. The solution wasvisually clear and free of particles. The solution was mixed at a 1:1volume ratio with RO water entering from the second inlet in thecontinuous flash mixer of FIG. 1 with an inlet diameter of 0.5 mm and aconical outlet leading to a tube diameter of 1 mm. The two solventstreams were at 25° C. through the inlet tubes. The size of thenanoparticles created by this process were controlled by adjusting theaverage velocity of the incoming stream between about 0.02 and 8.5meters per second as shown in FIG. 3. Mean particle size was observed tobe between about 22 nm and 55 nm depending on mixing velocity, withsmaller particles resulting with higher mixing velocities. Severalmilliliters of the process stream exiting the mixer at each operatingcondition were collected in a sample vial for analysis by photoncorrelation spectroscopy. Several samples at both high and low mixingrates were assayed after a period of two weeks and shown to have a sizewithin 6 nm of their original size, indicating a stable particle size.

Example 2 Nanoparticles of PS(1000)-b-PEO(3000) and β-Carotene in a 1:1Ratio in THF and Water Made in a Continuous Flash Mixer

This example demonstrates that a pharmaceutical compound, an antioxidantand a vitamin useful for mammal administration, can be formulated asnanoparticles using amphiphilic copolymers and a continuous flash mixerto yield a surface of PEO groups. This example also demonstrates thatthe nanoparticles produced by flash precipitation are sufficientlystable for post processing and subsequent formulation. One hundredpercent of the particles were less than 700 nm and the average particlesize was less than 400 nm.

A total of 3.32 grams of β-carotene, an additive target molecule, and3.32 grams PS(1000)-b-PEO(3000) were dissolved in 123 grams of THF at35° C. These charges correspond to 2.6 wt % copolymer, 2.6 wt % caroteneand a weight ratio of 1:1 for amphiphilic copolymer to additive targetmolecule. The solution was a deep red color and visually clear ofparticles. The process solvent stream was mixed with water, enteringfrom the second inlet at a volume ratio of 1:0.94 in the continuousflash mixer at a temperature of 35° C. Both streams entered the mixerthrough tubes 1 mm in diameter. The diameter of the mixing vessel was4.8 mm and the outlet was conical leading to an outlet tube 2 mm indiameter. The average velocity of the β-carotene stream was 2.8 m/scorresponding to a total solids (when dried) production rate of over 9kg/day, or a liquid processing rate (both streams) of over 340 kg/day.The total solids concentration of the mixer effluent after nanoparticleformation was approximately half the original value, or 2.6 wt %.

In a period of approximately 20 seconds, 90.5 grams of nanoparticleproduct effluent from the continuous flash mixer was collected in 444grams of agitating RO water and a well agitated sample was dilutedfurther with water to a concentration suitable for analysis. The yieldof nanoparticles below 1060 nm was 100% with a mean size of 0.37 μm asmeasured by a Malvern Mastersizer S. The particle size distribution ofthis example is shown in FIG. 4. The product was opaque and orange andno large particles were distinguishable by eye in any of the samplesdiluted for analysis or in the product stream. Three weeks later, asecond sample of the collected product stream was agitated and dilutedfurther with water and analyzed. The yield ofnanoparticles below 1060 nmwas over 99% as measured by a Malvern Mastersizer S with a mean size of0.42 mm.

Example 2A Nanoparticles of PS(1000)-b-PEO(3000) and β-Carotene in a 1:1Ratio in THF and Water Made in a Continuous Flash Mixer

A total of 4.6 grams of pcarotene and 4.6 grams PS(1000)-b-PEO(3000)were dissolved in 166 grams of THF at 35° C., corresponding to 2.6 wt %copolymer, 2.6 wt % β-carotene, and a weight ratio of 1:1 foramphiphilic copolymer to additive target molecule. The solution was adeep red color and visually clear of particles. The process solventstream was mixed with water, entering from the second inlet, at a volumeratio of 1:0.94 in the continuous flash mixer at a temperature of 35° C.(see FIG. 1). Both streams passed through the coil heat exchanger andentered the mixer through a 1 mm-tube. The pressure of the incomingstreams were controlled at 17 psig., and the receiver was at atmosphericpressure. The mixer chamber diameter was 4.8 mm and the outlet wasconical leading to an outlet tube of 2 mm. The average velocity of theprocess solvent stream was 4.3 m/s corresponding to a liquid processingrate of over 500 kg/day and a total solids when dried production rate ofover 13 kg/day. The total solids concentration of the mixer effluentafter nanoparticle formation was approximately half the original value,or 2.6 wt % and comprised 50% β-carotene.

In a period of approximately 10 seconds, 85 grams of nanoparticleproduct effluent from the continuous flash mixer was collected in 488grams of RO water in a separate holding tank and a well agitated samplewas diluted further with water to a concentration suitable for analysis.The yield of nanoparticles below 1060 nm was 100% with a mean size of0.36 μm as measured by a Malven Mastersizer S. The product was opaqueand orange and no large particles were distinguishable by eye in any ofthe samples diluted for analysis or in the product stream. Three monthslater without agitation in between, a second agitated sample of thecollected product stream was taken and diluted further with water andanalyzed. The yield of nanoparticles below 1060 nm was 100% as measuredby a Malvern Mastersizer S with a mean size of 0.40 μm. This resultindicated the sufficient stability of the nanoparticles was achieved toconduct additional post processing steps.

Example 2B Post Processing Treatment of Nanoparticles ofPS(1000)-b-PEO(3000) and β-Carotene

This example demonstrates a post processing process useful for theformulation of target molecules of a pharmaceutical for administrationas a liquid.

Approximately, half the effluent collected in Example 2A, 305 g, wasdistilled under reduced pressure at a temperature less than 70° C. Atotal of 3.3 volumes of RO waterwas added portion-wise in four partsbringing the concentration to the starting value prior to the nextaddition. The final concentration was the same as the original and theresulting particle size distribution of this example was measured thenext day with results as shown in FIG. 5. The yield ofnanoparticlesbelow 1060 nm was 100% with a mean size of 0.36 μm as measured by aMalvern Mastersizer S and with a average size less than 400 nm.

Example 2C Filtration and Lyophilization of Nanoparticles

A 1.2 μm (nominal) nylon syringe filter was dried under vacuum at 80° C.A portion of the nanoparticle product of example 2B, after the postprocessing treatment to remove solvent and after aging the material atroom temperature for 11 weeks in a sealed bottle in a quiescent state,was agitated and filtered through the same 1.2 μm nylon filter at roomtemperature followed by a RO water wash of 0.18 volumes. A total of 177mg of sucrose was added to the filtrate and the combination waslyophilized to obtain 300 mg of a solvent and aqueous free powder.Meanwhile, the filter was again dried under vacuum at 80° C. and lessthan 1 mg of product was caught on the filter, less 1% of thenanopaticles present. No microparticles were visible to the eye on thefilter. A sample of the filtrate after the addition of sugar analyzed bythe Mastersizer S showed essentially the same particle size as measuredpreviously; 100% of the particles were <1060 nm in diameter and had amean size of 0.36 μm.

Example 3 Nanoparticles of PS(1000)-b-PEO(3000) and β-Carotene in a1:6.5 Ratio in THF and Water Made in a Continuous Flash Mixer

Several nanoparticle solutions were prepared from process solventcontaining 0.40 wt % PS(1000)-b-PEO(3000) and 2.6 wt % β-carotenecopolymer with a weight ratio of 1:6.5 for amphiphilic copolymer toadditive target molecule in THF at 35° C. using water as the non-processsolvent The mxing velocities for each process are presented in Table 1below. Final nanoparticle solutions were diluted in water and agitatedfor measurement.

The total solids concentration of the mixer effluent after nanoparticleformation was 1.5 wt %. The nanoparticle product stream was added to ROwater in the agitated vessel at a ratio of 1:4 to 1:6. This mixture wasthen diluted again with water to a concentration appropriate forparticle size analysis using the Mastersizer S.

TABLE 1 PS(1000)-b- Mixing Liquid β-carotene PEO(3000) THF VelocityProduct H₂O (g) (g) ratio (g) (m/sec) (g) (g) 2.72 0.416 6.54 102 0.30na 160 2.4 0.36 6.67 88 0.90 82.6 444 2.72 0.416 6.54 102 1.27 43.3 1602.83 0.44 6.40 108 1.70 95.6 444 4.93 0.753 6.55 184 2.84 86.5 444 6.180.96 6.44 231 4.27 52.6 248 6.18 0.96 6.44 231 4.27 26.15 175

The average velocity of the stream containing the copolymer and targetmolecule was between about 0.9 to 4.3 m/sec and the resultingnanoparticles characteristics are displayed in FIG. 5 with mostparticles displaying an average diameter of <0.5 μm and all particleshaving an average diameter of <0.1 μm. The nanoparticle production rate(dry solids content) reached over 7.5 kg/day and the fluid processingrate exceeded 500 kg/day. The total solids concentration of the mixereffluent after nanoparticle formation was approximately half theoriginal value, or 1.5 wt % and comprised 85% target molecule by weight.

Higher velocities produced higher yields of nanoparticles or a smallernanoparticle size as shown in FIG. 6. The stability of the run at avelocity of 4.3 m/sec was tested two weeks later and found to beacceptable for post processing, a total of 91% of the particles wereless than 1060 nm in diameter. These examples demonstrate sparingquantities of the amphiphilic copolymer can be used to afford thedesired nanoparticle production.

Example 3B Nanoparticles of PS(1000)b-PEO(3000) and β-Carotene in a1:6.5 Ratio in THF and Water Made in a Continuous Flash Mixer

The conditions of Example 3 were the same except that the mixingvelocity was 0.30 m/s. At this velocity, the mixer plugged withparticles since the particles were formed at a size a large fraction ofparticles were formed at a size significantly larger than 1 μm.

Example 4 Nanoparticles of PS(1000)-b-PEO(3000) and β-Carotene in a1:6.5 Ratio in THF and Water Made in a Batch Flash Mixer

The purpose of this example was to demonstrate a flash mixer in a batchconfiguration could be used to create nanoparticles of a poorlywater-soluble pharmaceutical compound useful for administration tomammals. The example was also conducted to demonstrate the mixingvelocity for the flash precipitation can be represented by a movingsurface.

The THF solvent stream contained dissolved 0.40 wt %PS(1000)-b-PEO(3000) copolymer and 2.6 wt % β-carotene, a weight ratioof 1:6.5:1 for amphiphilic copolymer to additive target molecule. Theprocess solvent was fed from a syringe pump through a coiled stainlesssteel tube ⅛^(th) inches in diameter and submersed in a water bath at35° C. Within 10 inches after exiting the bath, the tube entered themixing vessel containing RO water and was connected to a tube 1 mm indiameter tube below the water surface. The process solvent was fed intothe zone of high intensity of the mixing vessel within 3 mm of amechanical agitator.

The fluid jet velocity of the process solvent exiting the inlet tube wasvaried between 0.26 m/s and 4.1 m/s and the mechanical agitator tipspeed was varied between 0.26 m/s and 4.1 m/s. Each combination of jetvelocity and tip speed is presented in FIG. 6 with the greatest volumepercent of particles having a diameter of <1060 nm when the jet velocityand agitator tip speed were high. The organic stream was charged to 180grams of RO water at 35° C. to a volume ratio with the exception ofExample ID 62 in which the charge was 128 grams. The data in FIG. 7 wascollected by further dilution of the batch product stream to thatappropriate for analysis by the Mastersizer S. At the lowest mixingvelocity evaluated, 0.26 m/sec, 18% of the particles were less than 1060nm in diameter. All other mixing velocities produced more than 65 volume% of particles less than 1060 nm with the greatest amount of particlesless than 1060 nm at 87 volume % and a volume mean size of 0.65 μm. Ahigh ratio of additive target molecule to amphiphilic copolymer was usedand the product stream can be produced at a high concentration (0.9 wt %solids on a dry basis of which over 85% was target molecule as shown inExample ID 66).

As with the continuous flash mixer, a threshold mixing velocity isrequired to ensure that over 65% of the nanoparticles by volume are lessthan 1060 nm in diameter. In addition, the mixing velocity of theagitator and the fluid jet velocity can affect the volume % ofnanoparticles that are less than 1060 nm. For equipment agitated bymechanical means, the mixing velocity characteristic of the movingsurfaces provides a rapid mixing time and causes flash precipitation.

Example 5 β-carotene in THF with no Amphiphilic Copolymer

Two solutions of THF were made with 2.6 wt % β-carotene. One solutioncontained THF and β-carotene only and the other contained 0.4 wt % of acommon surfactant, the poloxamer, F87® (polyoxypropylene/polyoxyethyleneavailable from BASF), of the type used for pharmaceutical applications.The average jet velocity was 1.4 m/s and the agitator tip speed was 1.4m/s for both solution examples. The process solvent was charged througha 1 mm tube, within 3 mm of the agitator, to 180 grams of RO water at35° C. or 38° C., and to a volume ratio of 8:1 non-process solvent toprocess solvent. In the absence of any copolymer or surfactant, only 9%of the Pcarotene particles were less than 1060 nm and the volume meanwas 120 μm. Addition of the surfactant, F87, produced only 18% of theparticles with a diameter of less than 1060 nm with a mean size of 140μm.

As demonstrated by average particle size greater than 100 βm, usingcommon surfactants or without using any additive, did not constitute aflash precipitation to produce a high yield of nanoparticles.

Example 6 PS(1000)-b-PEO(3000) and β-Carotene in a 1:6.5 Ratio in THFand Water Using Conventional Mixing

A THF solvent stream contained dissolved 0.40 wt % PS(1000)-b-PEO(3000)copolymer and 2.6 wt % β-carotene with a weight ratio of 1:6.5 foramphiphilic copolymer to additive target molecule. The process andnon-process solvents were mixed by conventional means at 33° C., bypouring a total of 19.8 grams of the process solvent into 182 grams ofRO water in a beaker with moderate agitation (magnetic stirrer, near 30mm, at approximately setting of 4.3 on a scale of 1-6). The final volumeratio was 1:8.3 for process solvent to water. Mixing was completed in 20seconds. A sample of the batch was withdrawn and diluted with water to aconcentration appropriate for particle size analysis. The yield ofnanoparticles less than 1060 nm was 46% based on the Mastersizer Sanalysis. In both the final mixture and samples diluted for analysis,large particles were distinguishable by eye.

As demonstrated by this example, conventional means of mixing arelimited in their ability to produce nanoparticles containing targetmolecules.

Example 7 Nanoparticles ofPolybutylacrylate(7500)-b-polyacrylicacid(7500)(“PBA(7500)-b-PAA(7500)”) in Methanol (“MeOH”) precipitated withMeOH/Water in a Continuous Flash Mixer

This example demonstrates the production of nanoparticles of amphiphiliccopolymers where the soluble exterior surface constitutes a mucoadherentand the formed nanoparticles. The concentration of amphiphilic copolymerwas increased and still produced a consistent and controlable size ofnanoparticles when a commensurate increase in the mixing velocity wasimposed.

Solutions of MeOH containing the amphiphilic block copolymerPBA(7500)-b-PAA(7500) were prepared at a concentrations ranging from of0.10 to 0.65 wt %. At 35° C., the solutions were visually clear and freeof particles. The solutions were mixed with either water or a water/MeOHmix at 35° C. using a continuous flash mixer. The process andnon-process solvents were fed through thin walled stainless steel tubing⅛^(th) inches in diameter and coiled in a water bath and to the mixer ofFIG. 1 with tube diameters of 0.5 mm, D/d of 4.8 and δ/d of 2.

The resulting average nanoparticle size was dependent on the mixingvelocity and ranged from about 25 nm to about 60 nm for nanoparticlesprecipitated with water and from about 35 nm to 65 nm for nanoparticlesprecipitated with a water/MeOH non-process solvent. The distribution ofnanoparticle size based on mix velocity and mean particle size ispresented in FIG. 8 and FIG. 9. At the highest velocity, a criticalprocess was obtained and the smallestnanoparticles were produced. Theresulting particles were stable, changing in size less than 6 nm over aperiod of 3 months.

Example 7A PBA(7500)-b-PAA(7500) in MeOH precipitated with Water UsingConventional Means

The same 0.25 wt % solution of PBA(7500)-b-PAA(7500) mixed with waterand MeOH using conventional means. A total of 1.66 grams ofPBA(7500)-b-PAA(7500) was mixed with 1.76 g of 64.5% methanol and water,a ratio of 1:0.93 by volume. The methanol and water were poured into theflask containing the copolymer and mixed with moderate agitation byhand. The resulting nanoparticles had an average diameter of 85 nm asshown in FIG. 8.

As demonstrated by the example, conventional mixing did not formnanoparticles at the size and yield obtained in the continuous flashmixer.

Example 8 Nanoparticles ofPolybutylmethacrylate(1000)-b-Polyethyleneoxide(3000)(“PBMA(1000)-b-PEO(3000)”) and β-Carotene in a 1:1 Ratio in THF andWater Made in a Continuous Flash Mixer

A total of 4.6 grams PBMA(1000)-b-PEO(3000) and 4.6 grams of β-carotenewere dissolved at 35° C. in 166 grams of THF. These charges correspondto 2.6 wt % copolymer, 2.6 wt % β-carotene and a weight ratio of 1:1 foramphiphilic copolymer to additive target molecule. The solution was adeep red color and visually. clear of particles. The process solventstream was mixed with water, entering from the second inlet, at a volumeratio of 1:0.94 in the continuous flash mixer at a temperature of 35° C.Both streams passed through the coil heat exchanger and entered themixer through a 1 mm-tube. The pressure of the incoming streams werecontrolled at 9 psig., and the receiver was at atmospheric pressure. Themixer chamber diameter was 4.8 mm. In a period of approximately 10seconds, 55 grams of effluent were collected in 304 grams of RO water.The resulting nanoparticles of organic active were 97%<1060 nm with aaverage or mean size D[4,3] of 0.45 μm.

Example 9 Nanoparticles of PS(1000)-b-PEO(3000) and β-Carotene in THFand Water Made in a Centripetal Mixer

A solution of 0.4 wt % PS(1000)-b-PEO(3000) copolymer and 2.6 wt %β-carotene in THF was made with 0.73 g PS(1000)-b-PEO(3000), 4.75 gβ-carotene, and 178 g THF with a weight ratio of 1:6.5 for amphiphiliccopolymer to additive target molecule. The process solvent stream wasmixed with water at 35° C., both of which were adjusted to 35° C. usinga coil heat exchanger and through inlets of similar dimensions. Thestreams were introduced at a volume ratio of 1:3.0 to 1.6.0 process tonon-process solvent in three separate mixing experiments in thecentripetal mixer pictured in FIG. 10. A syringe pump was used for theprocess stream which was delivered at a pressure of 2.5 or 4.5 psig. Thenon-process solvent, RO water, was supplied to the centripetal mixerfrom a pressurized vessel delivered to the mixer at a pressure of 20-21psig. The velocity of the process solvent stream entered at a meanvelocity of 0.24 m/s to 0.44 m/s and the non-process stream entered at amean velocity of 1.3 mls.

In this mixer, the streams do not collide but are stretched as theycirculate and eventually pushed through the exit hole in the bottom ofthe mixer. The ratio of dimensions in the mixer was D/8=4, H/δ=1 andw/δ=0.8 representing a highly confined mixer. For each mixture, aportion of the effluent stream out of the mixer was collected in areceiving vessel consisting of an empty bottle. The product was opaqueand orange and no large particles were distinguishable by eye. Analysisseveral hours later by the Mastersize S showed a yield of 89 to 87% ofthe particles by volume were <1060 nm and the mean particle size wasD[4,3]=0.6 μm.

As shown in FIG. 10, a number of flow ratios can be used to produce asimilar yield and average size of nanoparticles. Although the mixingvelocity of the process solvent was changed, the non-solvent mixingvelocity was held constant and the particles size was controlled by thevelocity of the higher velocity stream. Likewise, in a confined mixer,the stream need not directly impact each other to obtain a good yield ofnanoparticles.

Example 10 Nanoparticles of PS(1000)-b-PEO(3000) and β-Carotene in a1:6.5 Ratio in THF and Water Made in a Continuous Flash Mixer—FinalProduct mixed With and Without Sodium Dodecyl Sulfate (“SDS”)

This example demonstrates that the addition of supplemental additivesinto thenanoparticle product stream can enhance the resulting productproperties, such as long term stability of the particles.

Two separate vessels were attached to a continuous flash mixer tocollect the nanoparticles produced from a flash precipitation ofβ-carotene and PS(1000)-b-PEO(3000) in THF and water. A total of 248 gof RO water was placed in one holding vessel and a total of 175 grams ofRO water and 0.87 grams of a supplemental additive useful for posttreatment, SDS (Sigma), was placed in a separate holding vessel.

A total of 0.96 g PS(1000)-b-PEO(3000) and 6.18 grams of β-carotene andwere dissolved in 231 g of THF at 35° C., corresponding to 0.4 wt %copolymer, 2.6 wt % β-carotene and a weight ratio of 1:6.5 foramphiphilic copolymer to additive target molecule. The solution was adeep red color and visually clear of particles. The volume ratio ofprocess solvent to non-process solvent was 1:0.94 for each mixture andboth solvents were held at a temperature of 35° C.

Both the process and non-process solvent streams passed through the coilheat exchanger and entered the mixer through a tube of 1 mm. Thepressure of the incoming streams were controlled at an average of 17psig. and the mixing vessel was at atmospheric pressure. The mixingvessel diameter was 4.8 mm and the outlet was conical leading to anoutlet tube of 2 mm and then to a transport tube of ⅛″ Teflon for 8inches before emptying into a product collection receiver. The averagevelocity of the process stream was 4.3 m/s. The total solidsconcentration of the mixer effluent after nanoparticle formation wasapproximately half the original value, or 1.5 wtl/o and comprised 85%target molecule by weight.

In a period of approximately 10 seconds, 52.6 grams of nanoparticleproduct effluent was collected from the continuous flash mixer intocontaining RO water only while agitating the contents. A well agitatedsample was diluted further with water to a concentration suitable foranalysis. The yield of nanoparticles below 1060 nm was 96% as measuredby a Malvern Mastersizer S (volume %). The product was opaque and orangeand no large particles were distinguishable by eye in any of the samplesdiluted for analysis or in the product stream. Fifteen days later, asecond agitated sample of the collected product stream was taken anddiluted further with water and analyzed. The yield of nanoparticlesbelow 1060 nm was 91% as measured by a Malvern Mastersizer S.

Intermediately after collecting nanoparticles in Vessel 1, a total of26.15 grams of nanoparticle were collected into the holding vesselcontaining SDS and RO water. A well agitated sample was diluted furtherwith water to a concentration suitable for analysis. The yield ofnanoparticles below 1060 nm was essentially the same, 97% as measured bya Malvern Mastersizer S (volume %), as that collected in Vessel 1. Theproduct was opaque and orange and no large particles weredistinguishable by eye in any of the samples diluted for analysis or inthe product stream. Fifteen days later, a second agitated sample of thecollected product stream was taken and diluted further with water andanalyzed. The yield of nanoparticles below 1060 nm was still 97% asmeasured by a Malvern Mastersizer S.

Example 11 Nanoparticles of PS(1000)-b-PEO(3000) and β-Carotene in a 2:1Ratio in THF and Water Made in a Continuous Flash Mixer

This example demonstrates a high yield of nanoparticles when the ratioof amphiphilic copolymer to target molecule is over 1:1 and the quantityof target molecule in the product stream on a dry weight basis can beadjusted over a wide range.

Two separate vessels were prepared to collect the nanoparticles streamfrom the continuous flash mixer. A total of 332 g of RO water was placedin one vessel and a total of 162 grams of RO water was placed in theother.

A total of 3.93 g PS(11000)-b-PEO(3000) were dissolved in 69.7 g of THFat 35° C. to visually clear state, then a total of 1.95 grams ofβ-carotene was added to this mixture, corresponding to 5.2 wt %copolymer, 2.6 wt % β-carotene, and a weight ratio of 2:1 for copolymerto β-carotene. The solution was a deep red color and visually clear ofparticles. The process solvent was mixed with water, entering from thesecond inlet, at a volume ratio of 1:0.96 in the continuous flash mixerat a temperature of 35° C. Both streams passed through the coil heatexchanger and entered the mixer through a tube of 1 mm. The mixerchamber diameter was 4.8 mm and the outlet was conical leading to anoutlet tube of 2 mm. The average velocity of the β-carotene streamduring the run was 2.8 m/s. The total solids concentration of the mixereffluent after nanoparticle formation was approximately half theoriginal value, or 3.9 wt % and comprised 33% target molecule by weight.

In a period of approximately 10 seconds, 43 grams of nanoparticles fromthe continuous flash mixer were collected in 332 grams of RO water in aseparate holding tank and agitated. A sample of this solution wasdiluted further with water to a concentration suitable for analysis. Theyield of nanoparticles below 1060 nm was 100% with a mean size of 0.34μm as measured by a Malvern Mastersizer S. The product was opaque andorange and no large particles were distinguishable by eye in any of thesamples diluted for analysis or in the product stream.

Comparing this example to Example 1 and Example 3, it is apparent thatnanoparticles can be made over a wide range of amphiphilic copolymers totarget molecule, 0%, 33%, and 85% target molecule in the product streamon a dry solids basis was demonstrated.

Example 11A Nanoparticles of PS(1000)-b-PEO(3000) and β-Carotene in a2:1 Ratio in THF and Water Made in a Continuous Flash Mixer—Effect ofMixing Time

Immediately after collecting the sample for Example 11, the ratio ofmixing for process and no-process solvent streams was changed to 1:0.93and the velocity of the process solvent was also changed to 0.42 m/secwith all other conditions the same. A total of 28.5 grams ofnanoparticle product was collected from the continuous flash mixer in162 grams of RO water in a separate holding tank and was agitated. Asample was diluted with water to a concentration suitable for analysis.The yield of nanoparticles below 1060 nm was 93% with a mean size of0.52 μm as measured by a Malvern Mastersizer S. The product was opaqueand orange and no large particles were distinguishable by eye in any ofthe samples diluted for analysis or in the product stream. This exampleshows that the mixing velocity can control the particle sizedistribution.

Example 12 Nanoparticles of PS(1000)-b-PEO(3000) and β-Carotene Made ina Continuous Flash Mixer to Produce Nanoparticles <200 nm

This example demonstrates nanoparticles of an amphiphilic copolymer anda pharmaceutical target molecule can form nanoparticles with an averagesize well below 200 nm and even below 100 nm. It also demonstrates thatthe mixing velocity can control the particle size and the particles aresufficiently stable for post processing.

Three vessels were connected to a continuous flash mixer and filled with332 g, 162 g, 124 g of RO water, respectively for dilution of theproduct stream prior to analysis.

A total of 0.49 g PS(1000)-b-PEO(3000) and 0.49 g of β-carotene weredissolved in 92 g of THF at 25° C., corresponding to 0.53 wt % copolymerand 0.53 wt % β-carotene and a weight ratio of 1:1. The solution was ared color and visually clear of particles. The process stream was mixedwith water, entering from the second inlet, at a volume ratio of 1:0.96,1:0.93 and 1:0.93, respectively, into the continuous flash mixer ofFIG. 1. Both the process solvent and non-process solvent streams weremaintained at 35° C. The total solids concentration of the mixereffluent after nanoparticle formation was approximately half theoriginal value, or 0.26 wt % and comprised 50% β-carotene.

One immediately after the other, the average velocity of process streamwas changed from 2.8 m/s to 1.3 m/s to 0.42 m/s and the water stream waschanged commensurately to maintain a ratio of 1:0.96, 1:0.93 and 1:0.93,respectively. A portion of the effluent, 42.6 g, 24.8 g, 26.7 g at eachof these velocities were collected in separate vessels. The particlesize distribution was too small to obtain reliable results with aMastersizer S. The resulting particle size was analyzed by photoncorrelation spectroscopy yielding a nanoparticle size of 90 nm, 110 nm,and 160 nm in diameter, respectively. All samples were light orange,opalescent, and clear to the eye without any large particles present,consistent with particles less than 200 nm in size. Seven days later,the samples had essentially the same particle size, within 4%, as afterformation.

Example 13 Nanoparticles of PS(1000)-b-PEO(3000) and and β-Carotene withLecithin and Sterile Filtered Ntbk PM4-1C)

This example demonstrates the formation of nanoparticles of anamphiphilic copolymer and a pharmaceutical target molecule with asupplemental additive and purified by filtration.

A total of 0.164 g of lecithin (Epikuron™ 200), a phospholipid additiveof the type commonly used in parenteral injections or liquidformulations, was added to 102 g of THF. The material dissolved to avisually clear solution of a pale yellow color. A total of 0.40gPS(1000)-b-PEO(3000) copolymer and 0.56 g of β-carotene were added tothe solution and dissolved at room temperature to a clear red solutionfree of particles. This process solvent stream containing an additive inaddition to an amphiphilic copolymer with the target molecule was loadedinto 100 mL syringes. RO water was also loaded into a separate set of100 mL syringes. The two solutions were mixed at a ratio of 1:0.95 forprocess solvent to process non-solvent in a continuous mixer of thestyle in FIG. 1, with inlet tubes of 0.5 mm a D/d of 4.8, a δ/d of 2,and a conical outlet. The average pressure of the two inlet streams was27 psig. The process solvent was fed to the mixer at a temperature of 54C. by adjusting the temperature from 23 C. using a ⅛″ coil submersed ina temperature bath. The non-process solvent was fed to the mixer at atemperature of 8 C. by adjusting the temperature from 23 C. using a ⅛″coil submersed in a separate temperature bath. The mixing velocity was11.4 m/s.

At steady state, a portion of the effluent from the mixer was collectedin a vessel containing 239 g of RO water. The sample were light orange,opalescent, and clear to the eye without any large particles present. Aportion was diluted firther with RO water to a concentration suitablefor analysis by laser photon correlation spectroscopy. The nanoparticlessize was 83 nm in diameter. A portion was filtered for sterilization ona 0.22 μm PVDF filter and diluted further for analysis by photoncorrelation spectroscopy. The nanoparticles size was essentially thesame, within 4%, 82 nm in diameter.

We claim:
 1. A process for preparing nanoparticles by flashprecipitation comprising: dissolving at least one amphiphilic copolymerand at least one organic additive target molecule in an organic solvent,wherein the additive target molecule to amphiphilic copolymer ratio byweight is at least 1:4, wherein said amphiphilic copolymer is apolystyrene-block-polyethyleneoxide; flash precipitating nanoparticlescomprising said at least one amphiphilic copolymer and said at least oneorganic additive target molecule by mixing the organic solventcomprising the amphiphilic copolymer and at least one organic additivetarget molecule with water or an aqueous solution comprising a bufferingagent or salt, wherein the particle size of the resulting nanoparticlesis a function of the temperature, the hydrophobic and hydrophiliccharacter of at least one amphiphilic copolymer, and the mixing velocityof the process, and wherein the mixing velocity of the organic solventand the water or aqueous solution is at least 0.1 m/sec.
 2. The processof claim 1, wherein at least one amphiphilic copolymer is comprised ofblocks with a minimum contour length equal to the length of at least 5ethylene units.
 3. The process of claim 1, wherein at least oneamphiphilic copolymer is comprised of blocks with a molecular weight ofat least 300 g/mole.
 4. The process of claim 1, wherein at least oneamphiphilic copolymer has a total molecular weight between about 1000 toabout 50,000 g/mole.
 5. The process of claim 1, wherein at least oneamphiphilic copolymer has a total molecular weight of at least 2000g/mole.
 6. The process of claim 1, wherein at least one amphiphiliccopolymer exhibits a surface tension when dissolved in water of at least50 dynes/cm at a concentration of 0.1 weight percent (“wt %”) at 25° C.7. The process of claim 1, wherein the organic solvent is capable ofdissolving at least 0.1% of at least one amphiphilic copolymer byweight.
 8. The process of claim 1, wherein the organic solvent is anether or an alcohol.
 9. The process of claim 1, wherein the organicsolvent includes tetrahydrofuran.
 10. The process of claim 1, whereinthe concentration of at least one amphiphilic copolymer in the organicsolvent is at least 0.1 wt %.
 11. The process of claim 1, wherein theconcentration of at least one amphiphilic copolymer in the organicsolvent is between about 0.3 wt % to about 10.0 wt %.
 12. The process ofclaim 1, wherein the concentration of at least one amphiphilic copolymerin the product solvent is at least 0.05 wt %.
 13. The process of claim1, wherein the temperature of the organic solvent and the water oraqueous solution is maintained between about 20° C. to about 50° C. 14.The process of claim 1, wherein the temperature of the organic solventand the water or aqueous solution is maintained at 35° C.
 15. Theprocess of claim 1, wherein the pressure during mixing is controlled.16. The process of claim 1, wherein the pressure during mixing ismaintained above 8 psig.
 17. The process of claim 1, wherein thenanoparticles are produced continuously.
 18. The process of claim 1,wherein the organic solvent is a liquefied gas.
 19. The process of claim1, wherein the aqueous solution is a liquefied gas.
 20. The process ofclaim 1, wherein the average size of the resulting nanoparticles is lessthan about 150 nm.
 21. The process of claim 1, further comprising thestep of removing the solvent from the product solvent containing thenanoparticles.
 22. The process of claim 21, wherein the product solventis removed by a process selected from the group consisting offiltration, distillation, evaporation, expansion, lyophilization, andextraction.
 23. The process of claim 1, wherein the additive targetmolecule to amphiphilic copolymer ratio by weight is 1:4 to about 20:1.24. The process of claim 1, wherein at least one organic additive targetmolecule make up at least 0.2% by weight of the mixture based on initialcharges to the mixer.
 25. The process of claim 1, wherein at least oneorganic additive target molecule is selected from the group consistingof pharmaceutical organic actives and pharmaceutical organic precursorcompounds.
 26. The process of claim 1, wherein at least one organicadditive target molecule is selected from the group consisting ofcyclosporins, immunoactive agents, analgesics, anti-inflammatory agents,anthelmintics, anti-arrhythmic agents, antibiotics, anticoagulants,antidepressants, antidiabetic agents, antiepileptics, antihistamines,antihypertensive agents, antimuscarinic agents, antimycobacterialagents, antineoplastic agents, immunosuppressants, antithyroid agents,antiviral agents, anxiolytic sedatives, astringents, beta-adrenoceptorblocking agents, blood products and substitutes, cardiac inotropicagents, contrast media, corticosteroids, cough suppressants, diagnosticagents, diagnostic imaging agents, diuretics, dopaminergics,haemostatics, immunological agents, lipid regulating agents, musclerelaxants, parasympathomimetics, parathyroid calcitonin andbiphosphonates, prostaglandins, radio-pharmaceuticals, sex hormones,anti-allergic agents, stimulants and anoretics, sympathomimetics,thyroid agents, vasodilators, xanthines, anti-oxidants, preservatives,vitamins, and nutrients.
 27. The process of claim 1, wherein at leastone organic additive target molecule is a protein.
 28. The process ofclaim 1, wherein at least one organic additive target molecule is anantioxidant.
 29. The process of claim 1, wherein at least one organicadditive target molecule is a water insoluble vitamin.
 30. The processof claim 1, wherein at least one organic additive target molecule isselected from the group consisting of agricultural organic compounds,biocides, pesticides, herbicides, fungicides, and insecticides.
 31. Theprocess of claim 1, wherein at least one organic additive targetmolecule is selected from the group consisting of cosmetic products,dyes, reagents, salts, biological markers, magnetic particle precursors,and radiopaque materials.
 32. The process of claim 1, wherein at leastone organic additive target molecule is β-carotene.
 33. The process ofclaim 1, wherein at least 85% of the resulting nanopartcles are <1060 nmin diameter.
 34. The process of claim 1, wherein at least one organicadditive target molecule is incorporated into the nanoparticle.
 35. Theprocess of claim 1, wherein at least one organic additive targetmolecule is selected from the group consisting of a crystalline phasedrug and an amorphous phase drug.
 36. The process of claim 1, furthercomprising the step of adding at least one supplemental additive to theorganic solvent before mixing or to the product solvent after mixing.37. The process of claim 36, wherein at least one supplemental additiveis selected from the group consisting of surfactants, gelatin,phospholipid, and pluronics.
 38. The process of claim 36, wherein atleast one supplemental additive is selected from the group consisting ofinert diluents, solubilizing agents, emulsifiers, suspending agents,adjuvants, wetting agents, colloidal dispersants, cellulose, dicalciumphosphate, dodecyl trimethyl ammonium bromide, glycerol, glycerolmonostearate, glucose, p-isononylphenoxypolt-(glycidol), glucamides,lecithin (phosphatides), maltosides, magnesium stearate, magnesiumaluminum silicate, oils, starch, polyethylene glycols, polyoxyethylenealkyl ethers, polyoxyethylene sorbitan fatty acid esters, poloxamers,polaxamines, silicic acid, sodium citrate, sodium dodecyl sulfate,sodium lauryl sulfate, steric acid, sucrose, tapioca starch, talc,thioglucosides, tragacanth, triethanolamine, and Triton X-200®.
 39. Theprocess of claim 36, wherein at least one supplemental additive is addedat a concentration by weight of up to 2:1 of supplemental additive toadditive target molecule.
 40. The process of claim 36, wherein at leastone supplemental additive is sodium dodecyl sulfate.
 41. The process ofclaim 36, wherein at least one supplemental additive is selected fromthe group consisting of a salt, a functional surface modifier, aprotein, a sugar, a fatty acid, an organic pharmaceutical excipient, aninorganic pharmaceutical excipient, a pharmaceutically acceptablecarrier, and a low molecular weight oligomer.
 42. The process of claim1, wherein the mixing step and flash precipitation step are performed ina centripetal mixer.
 43. The process of claim 1, wherein the mixing stepand flash precipitation step are performed in a continuous flash mixer.44. The process of claim 1, wherein the mixing step and flashprecipitation step are performed in a batch flash mixer.
 45. The methodof claim 1, wherein the mixing of the organic solvent with the water oraqueous solution comprises injecting the organic solvent and the wateror aqueous solution into a confined mixing chamber at the same time. 46.The method of claim 45, wherein the organic solvent and the water oraqueous solution are injected into the chamber at about 0.02 m/s to 12.0m/s.
 47. The method of claim 45, wherein said mixing chamber comprisesan outlet for continuous flow from said mixing chamber.
 48. The methodof claim 45, wherein the organic solvent and the water or aqueoussolution are injected at each other within said mixing chamber.
 49. Themethod of claim 45, wherein the organic solvent and the water or aqueoussolution are injected via separate inlet tubes.
 50. The method of claim49, wherein the distance between the inlet tubes within the mixingchamber is less than 40 times the diameter of the inlet tubes.
 51. Themethod of claim 1, wherein the additive target molecule to amphiphiliccopolymer ratio by weight is at least 1:2.
 52. The method of claim 1,wherein the additive target molecule to amphiphilic copolymer ratio byweight is at least 1:1.
 53. The method of claim 1, wherein the additivetarget molecule to amphiphilic copolymer ratio by weight is 1:4 to 10:1.